US20020004023A1 - Chloride assisted hydrometallurgical extraction of metal - Google Patents

Chloride assisted hydrometallurgical extraction of metal Download PDF

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US20020004023A1
US20020004023A1 US09/866,027 US86602701A US2002004023A1 US 20020004023 A1 US20020004023 A1 US 20020004023A1 US 86602701 A US86602701 A US 86602701A US 2002004023 A1 US2002004023 A1 US 2002004023A1
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pressure oxidation
copper
process according
raffinate
sulphate
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David Jones
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    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00Obtaining nickel or cobalt
    • C22B23/04Obtaining nickel or cobalt by wet processes
    • C22B23/0407Leaching processes
    • C22B23/0415Leaching processes with acids or salt solutions except ammonium salts solutions
    • C22B23/043Sulfurated acids or salts thereof
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00Obtaining copper
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00Obtaining copper
    • C22B15/0063Hydrometallurgy
    • C22B15/0065Leaching or slurrying
    • C22B15/0067Leaching or slurrying with acids or salts thereof
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00Obtaining copper
    • C22B15/0063Hydrometallurgy
    • C22B15/0065Leaching or slurrying
    • C22B15/0067Leaching or slurrying with acids or salts thereof
    • C22B15/0069Leaching or slurrying with acids or salts thereof containing halogen
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00Obtaining copper
    • C22B15/0063Hydrometallurgy
    • C22B15/0065Leaching or slurrying
    • C22B15/0067Leaching or slurrying with acids or salts thereof
    • C22B15/0071Leaching or slurrying with acids or salts thereof containing sulfur
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00Obtaining copper
    • C22B15/0063Hydrometallurgy
    • C22B15/0084Treating solutions
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B15/00Obtaining copper
    • C22B15/0063Hydrometallurgy
    • C22B15/0084Treating solutions
    • C22B15/0089Treating solutions by chemical methods
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00Obtaining nickel or cobalt
    • C22B23/04Obtaining nickel or cobalt by wet processes
    • C22B23/0407Leaching processes
    • C22B23/0415Leaching processes with acids or salt solutions except ammonium salts solutions
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00Obtaining nickel or cobalt
    • C22B23/04Obtaining nickel or cobalt by wet processes
    • C22B23/0407Leaching processes
    • C22B23/0415Leaching processes with acids or salt solutions except ammonium salts solutions
    • C22B23/0423Halogenated acids or salts thereof
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B23/00Obtaining nickel or cobalt
    • C22B23/04Obtaining nickel or cobalt by wet processes
    • C22B23/0476Separation of nickel from cobalt
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/04Extraction of metal compounds from ores or concentrates by wet processes by leaching
    • C22B3/06Extraction of metal compounds from ores or concentrates by wet processes by leaching in inorganic acid solutions, e.g. with acids generated in situ; in inorganic salt solutions other than ammonium salt solutions
    • C22B3/08Sulfuric acid, other sulfurated acids or salts thereof
    • CCHEMISTRY; METALLURGY
    • C22METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22BPRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/26Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00Technologies related to metal processing
    • Y02P10/20Recycling

Definitions

  • This invention relates to the hydrometallurgical treatment of metal ores or concentrates.
  • it relates to the extraction of copper from sulphide ores or other concentrates in the presence of halogen ions, such as chloride ions.
  • the purpose of the present invention is to provide an improved process for the extraction of metals from sulphide ores.
  • a process for the extraction of copper from a sulphide copper ore or concentrate comprising the steps of subjecting the ore or concentrate to pressure oxidation in the presence of oxygen and an acidic solution containing halide and sulphate ions to obtain a resulting pressure oxidation slurry, subjecting the slurry to a liquid/solid separation step to obtain a resulting pressure oxidation filtrate and a solid residue containing an insoluble basic copper sulphate salt; leaching the basic copper sulphate salt produced by the pressure oxidation with an acidic sulphate solution in a second leaching to dissolve the basic copper salt to produce a leach liquor containing copper sulphate in solution and a resulting solid residue; separating the leach liquor from the solid residue; subjecting the leach liquor to a solvent extraction process to produce copper concentrate solution and a copper depleted raffinate; recycling at least a portion of the raffinate to the pressure oxidation; and wherein the
  • concentrate in this specification refers to any material in which the metal value content has been increased to a higher percentage by weight as compared with the naturally occurring ore and includes man made artificial sulphide ore, such as matte, and metal values precipitated as solids such as hydroxides and sulphides.
  • FIG. 1 is a flow diagram of a hydrometallurgical metal extraction process according to one embodiment of the invention.
  • FIG. 2 is a flow diagram of a hydrometallurgical metal extraction process according to another embodiment of the invention.
  • the feed ore or concentrate to the process may contain one or more sulphide minerals of the base metals Cu, Ni, Co and Zn, frequently combined with Fe and sometimes with other elements, such as As, Sb, and Ag.
  • reference numeral 10 generally indicates a hydrometallurgical process according to one embodiment of the invention.
  • the process 10 comprises a pressure oxidation stage 12 , an atmospheric leach 14 , a liquid/solid separation 24 , a solvent extraction 16 , an evaporation stage 20 and a neutralization 22 .
  • the copper concentrate Prior to the pressure oxidation stage 12 , the copper concentrate is first subjected to a regrind to reduce the particle size to about 2 %+325 mesh.
  • the concentrate is subjected to the pressure oxidation 12 in an autoclave in the presence of an acidic solution containing sulphate, chloride and preferably copper ions.
  • the amount of acid introduced into the pressure oxidation 12 is sufficient to maintain the discharge solution from the autoclave, when operated in a continuous mode, at a pH of above 2.0, typically pH 2.3-3.8.
  • the chloride ion concentration in the solution in the autoclave is maintained at about 8-20 g/L, preferably about 12 g/L.
  • the pressure oxidation 12 is carried out at a temperature of from about 115° C. to about 175° C., preferably about 130° C. to about 155° C., under a pressure of about 100-300 psig. This is total pressure comprising oxygen pressure plus steam pressure.
  • the retention time is about 0.5-2.5 hours and the process is normally carried out in a continuous fashion in the autoclave. However, the process can also be carried out in a batch-wise fashion, if desired.
  • the solids content in the autoclave is maintained at about 12-25%, i.e. 150-300 g/L solids as determined by the heat balance and viscosity limitations.
  • the slurry produced in the autoclave is discharged through a series of one or more flash tanks (not shown) to reduce the pressure to atmospheric pressure and the temperature to about 90-100° C.
  • the liquid part of the slurry is referred to as the product solution from the pressure oxidation stage 12 and is indicated by reference numeral 21 .
  • the solids from the pressure oxidation stage 12 after the filtration 24 are treated in the atmospheric leaching stage 14 at about pH 1.2 to pH 2.2 using raffinate from the solvent extraction 16 , which is acidic, to dissolve the basic copper sulphate.
  • the leaching 14 takes place at a temperature of about 40° C. for a retention time of about 15-60 minutes.
  • the percentage solids in the feed to the leach 14 is typically about 3-15% or about 30-170 g/L, although it is possible to operate the process outside this range.
  • the percentage solids drops substantially during the leach 14 as the basic copper sulphate dissolves.
  • the product g/L solids may be as little as one half of the feed g/L solids.
  • the basic copper salts dissolve almost completely with very little of the iron present in the concentrate going into solution, provided care is taken to maintain the pH in the range 1.2 to 2.2, preferably pH 1.5 to 2.0.
  • the slurry 31 from the atmospheric leaching stage 14 is sometimes difficult if not impossible to filter, but settles well.
  • the slurry 31 is pumped to a counter current decantation (CCD) wash circuit 34 .
  • CCD counter current decantation
  • the solids are fed through a series of thickeners with wash water added in the opposite direction.
  • wash water added in the opposite direction.
  • the solids are washed and entrained solution removed, together with the soluble metals dissolved therein.
  • About 3 to 7 thickeners are required with a wash ratio (water to solids) of about 2 to 5 to reduce entrained liquor down to less than 100 ppm dissolved Cu in the final residue.
  • the thickener underflow from the last thickener is the final residue stream 35 at about 50% solids. This can be treated for the recovery of precious metals, such as gold and silver, or sent to tailings.
  • the main constituents of the stream 35 are hematite and elemental sulphur, which may also be recovered by a combination of other processes, such as flotation and leaching into a specific solvent for sulphur, e.g. perchloroethylene, if market conditions warrant.
  • the thickener overflow from the first thickener is the product solution 33 which is fed to the solvent extraction stage 16 , as shown.
  • Copper is extracted from the product solution 33 from the CCD circuit 34 in two stages of extraction in the solvent extraction stage 16 to produce a raffinate 37 .
  • the raffinate 37 is split, as indicated at 38 , into three streams 40 , 41 and 42 .
  • the stream 40 which comprises about 2 ⁇ 3 of the raffinate 37 is recycled to effect the atmospheric leach 14 , as indicated above.
  • the actual volume of 40 is determined by the acid needs of the leach 14 , to dissolve the basic copper sulphate as described, and maintain a slight excess of acid, i.e. pH 1.5-2.0 which corresponds to about 1-5 g/L H 2 SO 4 .
  • the acid requirements for stream 40 are less than the total acid contained in 37 , and part of the remainder is used in the pressure oxidation 12 as an acid source for the reactions therein. This is supplied by stream 42 .
  • streams 41 and 42 are each about 1 ⁇ 6 of 37 .
  • the stream 41 which comprises about 1 ⁇ 6 of the raffinate 37 is subjected to the neutralization 22 with lime rock and after liquid/solid separation 43 results in gypsum, which can be discarded, and wash water which is recycled as wash water to the CCD wash circuit 34 .
  • the amount of water to be evaporated must be minimized.
  • the copper concentration in the stream 31 is maintained at a more concentrated level, i.e. at about 35 g/L, compared with a value of 12 g/L in the absence of evaporation. This in turn generates a more concentrated acid stream 42 containing about 48 g/L H 2 SO 4 instead of only 18 g/L H 2 SO 4 .
  • Direct fired evaporators do not have the advantage of multiple effect of the steam generated which can generally reduce fuel costs in indirect evaporators, and thus justify evaporating large volume of water.
  • the process 100 also comprises a pressure oxidation stage 12 , filtration 24 , atmospheric leach 14 , CCD wash circuit 34 , solvent extraction 16 , evaporation 20 and neutralization 22 .
  • the liquid 21 from the filtration 24 is subjected to a copper solvent extraction 50 in order to recover copper values therefrom.
  • the filtration 24 is the separation point between the high chloride liquid used in the pressure oxidation 12 , which liquid is recycled as indicated, and a low chloride or chloride free liquid going to the atmospheric leach 14 .
  • the filtration 24 is always accompanied by a wash with water or recycled low chloride water or a concentration of both to remove as much chloride from the solids (filter cake) as possible.
  • the objective is to minimize transfer of chloride from the high chloride circuit to the low chloride circuit, to counteract chloride build up in the latter circuit.
  • the stream 42 is subjected to the evaporation 20 , as described with reference to FIG. 1, prior to recycle to the pressure oxidation 12 .
  • there is no need to recycle acid from the low chloride circuit because enough acid is generated by the copper solvent extraction 50 in the form of raffinate 63 .
  • the neutralization product is subject to a liquid/solid separation step to produce solid gypsum which can be discarded and a liquid 66 which is subjected to the evaporation 20 before recycle.
  • the raffinate 37 from the solvent extraction 16 is split into only two streams, i.e. 2 ⁇ 3 into stream 40 which is used in the atmospheric leach 14 , and 1 ⁇ 3 into stream 41 which is subjected to the neutralization 22 and liquid/solid separation 43 to produce solid gypsum which can be discarded and a stream 45 which is split, as indicated at 46 into a stream which is recycled as wash water to the CCD circuit 34 and stream 42 which goes to the evaporation 20 for recycle to the pressure oxidation 12 .
  • This serves to recycle chloride from the low chloride circuit back to the high chloride circuit.

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Abstract

A process for the extraction of copper from a sulphide ore or concentrate comprises the steps of subjecting the ore or concentrate to pressure oxidation in the presence of oxygen and an acidic solution containing halide and sulphate ions to obtain a resulting pressure oxidation slurry. The slurry is subjected to a liquid/solid separation step to obtain a resulting pressure oxidation filtrate and a solid residue containing an insoluble basic metal sulphate salt. The basic metal sulphate salt is leached in a second leaching with an acidic sulphate solution to dissolve the basic metal salt to produce a leach liquor containing a metal sulphate, e.g. copper sulphate, in solution and a resulting solid residue. The leach liquor is separated from the solid residue and subjected to a solvent extraction process to produce metal concentrate solution and a metal depleted raffinate. At least a portion of the raffinate is recycled to the pressure oxidation after being subjected to evaporation.

Description

    CROSS REFERENCE TO RELATED APPLICATION
  • This application is a division of U.S. patent application Ser. No. 09/452,431 filed Dec. 1, 1999 which in turn is a division of U.S. patent application Ser. No. 08/911,797 filed Aug. 15, 1997. The contents of the foregoing applications are incorporated herein by reference.[0001]
  • FIELD OF THE INVENTION
  • This invention relates to the hydrometallurgical treatment of metal ores or concentrates. In particular, it relates to the extraction of copper from sulphide ores or other concentrates in the presence of halogen ions, such as chloride ions. [0002]
  • BACKGROUND OF THE INVENTION
  • The hydrometallurgical treatment of sulphide concentrates whereby the concentrate is subjected to pressure oxidation in the presence of chloride ions is known. See for example U.S. Pat. Nos. 4,039,406; 5,645,708; and 5,650,057. [0003]
  • The purpose of the present invention is to provide an improved process for the extraction of metals from sulphide ores. [0004]
  • SUMMARY OF THE INVENTION
  • According to the invention there is provided a process for the extraction of copper from a sulphide copper ore or concentrate, comprising the steps of subjecting the ore or concentrate to pressure oxidation in the presence of oxygen and an acidic solution containing halide and sulphate ions to obtain a resulting pressure oxidation slurry, subjecting the slurry to a liquid/solid separation step to obtain a resulting pressure oxidation filtrate and a solid residue containing an insoluble basic copper sulphate salt; leaching the basic copper sulphate salt produced by the pressure oxidation with an acidic sulphate solution in a second leaching to dissolve the basic copper salt to produce a leach liquor containing copper sulphate in solution and a resulting solid residue; separating the leach liquor from the solid residue; subjecting the leach liquor to a solvent extraction process to produce copper concentrate solution and a copper depleted raffinate; recycling at least a portion of the raffinate to the pressure oxidation; and wherein the raffinate is subjected to evaporation to remove water therefrom prior to the recycle thereof; and wherein the evaporation is effected by means of a direct-fired evaporation process comprising the submerged combustion of a fuel in the raffinate being recycled. [0005]
  • The term “concentrate” in this specification refers to any material in which the metal value content has been increased to a higher percentage by weight as compared with the naturally occurring ore and includes man made artificial sulphide ore, such as matte, and metal values precipitated as solids such as hydroxides and sulphides. [0006]
  • Further objects and advantages of the invention will become apparent from the description of preferred embodiments of the invention below. [0007]
  • BRIEF DESCRIPTION OF THE DRAWINGS
  • FIG. 1 is a flow diagram of a hydrometallurgical metal extraction process according to one embodiment of the invention. [0008]
  • FIG. 2 is a flow diagram of a hydrometallurgical metal extraction process according to another embodiment of the invention.[0009]
  • DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS
  • The feed ore or concentrate to the process may contain one or more sulphide minerals of the base metals Cu, Ni, Co and Zn, frequently combined with Fe and sometimes with other elements, such as As, Sb, and Ag. [0010]
  • In FIG. 1, [0011] reference numeral 10 generally indicates a hydrometallurgical process according to one embodiment of the invention. The process 10 comprises a pressure oxidation stage 12, an atmospheric leach 14, a liquid/solid separation 24, a solvent extraction 16, an evaporation stage 20 and a neutralization 22.
  • Prior to the [0012] pressure oxidation stage 12, the copper concentrate is first subjected to a regrind to reduce the particle size to about 2 %+325 mesh.
  • The concentrate is subjected to the [0013] pressure oxidation 12 in an autoclave in the presence of an acidic solution containing sulphate, chloride and preferably copper ions.
  • The amount of acid introduced into the pressure oxidation [0014] 12 (by way of recycle after the initial startup, as will be described below) is sufficient to maintain the discharge solution from the autoclave, when operated in a continuous mode, at a pH of above 2.0, typically pH 2.3-3.8.
  • The chloride ion concentration in the solution in the autoclave is maintained at about 8-20 g/L, preferably about 12 g/L. [0015]
  • The [0016] pressure oxidation 12 is carried out at a temperature of from about 115° C. to about 175° C., preferably about 130° C. to about 155° C., under a pressure of about 100-300 psig. This is total pressure comprising oxygen pressure plus steam pressure.
  • The retention time is about 0.5-2.5 hours and the process is normally carried out in a continuous fashion in the autoclave. However, the process can also be carried out in a batch-wise fashion, if desired. [0017]
  • In the [0018] pressure oxidation stage 12, all copper minerals are converted to basic copper sulphate CuSO4·2Cu(OH)2, i.e. all the copper being recovered reports to the solid phase in the pressure oxidation 12.
  • The solids content in the autoclave is maintained at about 12-25%, i.e. 150-300 g/L solids as determined by the heat balance and viscosity limitations. [0019]
  • The slurry produced in the autoclave is discharged through a series of one or more flash tanks (not shown) to reduce the pressure to atmospheric pressure and the temperature to about 90-100° C. The liquid part of the slurry is referred to as the product solution from the [0020] pressure oxidation stage 12 and is indicated by reference numeral 21.
  • The slurry from the flash tank(s) [0021] 22 is filtered, as shown at 24, and the resultant filter cake is washed thoroughly to remove entrained liquor as much as possible.
  • The solids from the [0022] pressure oxidation stage 12 after the filtration 24, are treated in the atmospheric leaching stage 14 at about pH 1.2 to pH 2.2 using raffinate from the solvent extraction 16, which is acidic, to dissolve the basic copper sulphate. The leaching 14 takes place at a temperature of about 40° C. for a retention time of about 15-60 minutes. The percentage solids in the feed to the leach 14 is typically about 3-15% or about 30-170 g/L, although it is possible to operate the process outside this range. The percentage solids drops substantially during the leach 14 as the basic copper sulphate dissolves. Thus, the product g/L solids may be as little as one half of the feed g/L solids.
  • During the [0023] atmospheric leaching stage 14, the basic copper salts dissolve almost completely with very little of the iron present in the concentrate going into solution, provided care is taken to maintain the pH in the range 1.2 to 2.2, preferably pH 1.5 to 2.0.
  • The [0024] slurry 31 from the atmospheric leaching stage 14 is sometimes difficult if not impossible to filter, but settles well. In view of the need to wash the leach solids very thoroughly, the slurry 31 is pumped to a counter current decantation (CCD) wash circuit 34. In the CCD circuit 34, the solids are fed through a series of thickeners with wash water added in the opposite direction. By this method, the solids are washed and entrained solution removed, together with the soluble metals dissolved therein. About 3 to 7 thickeners (not shown) are required with a wash ratio (water to solids) of about 2 to 5 to reduce entrained liquor down to less than 100 ppm dissolved Cu in the final residue.
  • The thickener underflow from the last thickener is the [0025] final residue stream 35 at about 50% solids. This can be treated for the recovery of precious metals, such as gold and silver, or sent to tailings.
  • The main constituents of the [0026] stream 35 are hematite and elemental sulphur, which may also be recovered by a combination of other processes, such as flotation and leaching into a specific solvent for sulphur, e.g. perchloroethylene, if market conditions warrant.
  • The thickener overflow from the first thickener is the [0027] product solution 33 which is fed to the solvent extraction stage 16, as shown.
  • Copper is extracted from the [0028] product solution 33 from the CCD circuit 34 in two stages of extraction in the solvent extraction stage 16 to produce a raffinate 37.
  • The raffinate [0029] 37 is split, as indicated at 38, into three streams 40, 41 and 42. The stream 40 which comprises about ⅔ of the raffinate 37 is recycled to effect the atmospheric leach 14, as indicated above. The actual volume of 40 is determined by the acid needs of the leach 14, to dissolve the basic copper sulphate as described, and maintain a slight excess of acid, i.e. pH 1.5-2.0 which corresponds to about 1-5 g/L H2SO4. The acid requirements for stream 40 are less than the total acid contained in 37, and part of the remainder is used in the pressure oxidation 12 as an acid source for the reactions therein. This is supplied by stream 42. Any acid still left over from 37, not used by 40 or 42, is considered excess, and is neutralized. This is stream 41. Typically streams 41 and 42 are each about ⅙ of 37. The stream 41 which comprises about ⅙ of the raffinate 37 is subjected to the neutralization 22 with lime rock and after liquid/solid separation 43 results in gypsum, which can be discarded, and wash water which is recycled as wash water to the CCD wash circuit 34.
  • The [0030] liquid 21 from the filtration 24, along with the stream 42, is subjected to the evaporation 20 to remove water and produce a more concentrated acid and chloride solution 44 which is recycled to the pressure oxidation 12.
  • The evaporation of the solution prior to recycling is problematical due to the very corrosive nature thereof, i.e. high acidity (50 g/L free acid), high chloride content (12 g/L) and high temperature in evaporation. This precludes the use of most if not all commercially available evaporators, which are normally based on indirect heat transfer through thin metal surfaces, such as shell and tube evaporators made typically of stainless steel. Titanium would be suitable but is too expensive if used in the large quantities which would be required for this type of application. [0031]
  • However, the problem has been solved by direct-fired evaporation using submerged combustion of a fuel in the [0032] solution 44 and using titanium material.
  • In order to keep the size of the evaporator down, and minimize operating and capital costs, the amount of water to be evaporated must be minimized. In order to achieve this, the copper concentration in the [0033] stream 31 is maintained at a more concentrated level, i.e. at about 35 g/L, compared with a value of 12 g/L in the absence of evaporation. This in turn generates a more concentrated acid stream 42 containing about 48 g/L H2SO4 instead of only 18 g/L H2SO4. This effectively reduces the volume of the water to be evaporated by putting the same mass of acid in a smaller volume of water, thus reducing the size of the evaporator, hence justifying the use of titanium, and the fuel costs necessary to operate a direct fired evaporator. Direct fired evaporators do not have the advantage of multiple effect of the steam generated which can generally reduce fuel costs in indirect evaporators, and thus justify evaporating large volume of water.
  • With reference to FIG. 2, a [0034] process 100 according to another embodiment of the invention is shown.
  • The [0035] process 100 also comprises a pressure oxidation stage 12, filtration 24, atmospheric leach 14, CCD wash circuit 34, solvent extraction 16, evaporation 20 and neutralization 22.
  • In the [0036] process 100 some of the metal values being recovered also report to the pressure oxidation liquid 21 in addition to the solid, which solid is subjected to the atmospheric leach 14 as described with reference to FIG. 1.
  • The liquid [0037] 21 from the filtration 24 is subjected to a copper solvent extraction 50 in order to recover copper values therefrom.
  • It should be noted that although the [0038] step 24 is referred to as a filtration, any suitable liquid/solid separation method can be employed.
  • The [0039] filtration 24 is the separation point between the high chloride liquid used in the pressure oxidation 12, which liquid is recycled as indicated, and a low chloride or chloride free liquid going to the atmospheric leach 14. The filtration 24 is always accompanied by a wash with water or recycled low chloride water or a concentration of both to remove as much chloride from the solids (filter cake) as possible. The objective is to minimize transfer of chloride from the high chloride circuit to the low chloride circuit, to counteract chloride build up in the latter circuit.
  • However, despite the washing of the solid residue produced by the [0040] filtration 24, the chloride concentration is prone to increase in the low chloride circuit, because it is essentially a dead ended circuit with minimum bleed.
  • This problem has been overcome by recycling a stream from the low chloride circuit to the high chloride circuit. This stream is indicated by [0041] reference numeral 42 in FIG. 2 to correspond with the stream 42 in FIG. 1 which also comprises a recycle from the low chloride circuit to the high chloride circuit.
  • Again the [0042] stream 42 is subjected to the evaporation 20, as described with reference to FIG. 1, prior to recycle to the pressure oxidation 12. However, in this case, there is no need to recycle acid from the low chloride circuit because enough acid is generated by the copper solvent extraction 50 in the form of raffinate 63. In fact, it is usually necessary to neutralize some of the acid in the raffinate 63, as indicated at 64 prior to recycling the raffinate 63. As indicated at 65, the neutralization product is subject to a liquid/solid separation step to produce solid gypsum which can be discarded and a liquid 66 which is subjected to the evaporation 20 before recycle.
  • Since there is no need to recycle acid from the low chloride circuit, the [0043] raffinate 37 from the solvent extraction 16 is split into only two streams, i.e. ⅔ into stream 40 which is used in the atmospheric leach 14, and ⅓ into stream 41 which is subjected to the neutralization 22 and liquid/solid separation 43 to produce solid gypsum which can be discarded and a stream 45 which is split, as indicated at 46 into a stream which is recycled as wash water to the CCD circuit 34 and stream 42 which goes to the evaporation 20 for recycle to the pressure oxidation 12. This serves to recycle chloride from the low chloride circuit back to the high chloride circuit.
  • While only preferred embodiments of the invention have been described herein in detail, the invention is not limited thereby and modifications can be made within the scope of the attached claims. [0044]

Claims (14)

What is claimed is:
1. A process for the extraction of copper from a sulphide copper ore or concentrate, comprising the steps of:
subjecting the ore or concentrate to pressure oxidation in the presence of oxygen and an acidic solution containing halide and sulphate ions to obtain a resulting pressure oxidation slurry, subjecting the slurry to a liquid/solid separation step to obtain a resulting pressure oxidation filtrate and a solid residue containing an insoluble basic copper sulphate salt;
leaching the basic copper sulphate salt produced by the pressure oxidation with an acidic sulphate solution in a second leaching to dissolve the basic copper salt to produce a leach liquor containing copper sulphate in solution and a resulting solid residue;
separating the leach liquor from the solid residue;
subjecting the leach liquor to a solvent extraction process to produce copper concentrate solution and a copper depleted raffinate;
recycling at least a portion of the raffinate to the pressure oxidation; and wherein
the raffinate is subjected to evaporation to remove water therefrom prior to the recycle thereof; and wherein
the evaporation is effected by means of a direct-fired evaporation process comprising the submerged combustion of a fuel in the raffinate being recycled.
2. The process according to claim 1, further comprising the steps of splitting the raffinate in at least two portions, wherein the one portion is recycled to the pressure oxidation and the other portion is recycled to the second leaching.
3. The process according to claim 1, further comprising the step of recycling the pressure oxidation filtrate to the pressure oxidation.
4. The process according to claim 3, further comprising the step of subjecting the pressure oxidation filtrate to evaporation to remove water therefrom prior to the recycle thereof to the pressure oxidation.
5. The process according to claim 4, wherein the evaporation is effected by means of a direct-fired evaporation process comprising the submerged combustion of a fuel in the filtrate being recycled.
6. A process according to claim 3, further comprising the steps of subjecting the pressure oxidation filtrate to a solvent extraction process, prior to the recycling of the filtrate, to produce a further copper concentrate solution and a further copper depleted raffinate which further copper depleted raffinate is recycled to the pressure oxidation.
7. The process according to claim 6, further comprising the step of subjecting the further copper depleted raffinate to neutralization prior to the recycling thereof to the pressure oxidation.
8. The process according to claim 1, wherein the pressure oxidation is carried out at a pH value of above about 2.
9. The process according to claim 8, wherein the pH in the pressure oxidation is from about 2.3 to about 3.8.
10. The process according to claim 1, wherein the second leaching is effected at a pH in the range of about 1.2 to about 2.2.
11. The process according to claim 10, wherein the pH in the second leaching is from about 1.5 to about 2.0.
12. The process according to claim 1, wherein the pressure oxidation slurry is flashed to atmospheric pressure at a temperature below the melting point of elemental sulphur.
13. The process according to claim 1, wherein the halide is selected from chloride and bromide.
14. The process according to claim 1, wherein the copper concentration in the leach liquor is maintained at a value of about 35 g/L.
US09/866,027 1997-08-15 2001-05-25 Process for the extraction of copper from a sulphide copper ore or concentrate Expired - Lifetime US6455019B2 (en)

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Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AU2008264193B1 (en) * 2008-08-11 2009-05-21 Jx Nippon Mining & Metals Corporation Process for recovery of copper from copper-containing chloride media
US20090241736A1 (en) * 2008-03-27 2009-10-01 Nippon Mining & Metals Co., Ltd. Method for recovering metal from ore
WO2013163712A1 (en) 2012-05-04 2013-11-07 Vale S.A. Sulfide ore leaching process
WO2014023755A1 (en) * 2012-08-10 2014-02-13 Basf Se Metal leach and recovery process
US20160331380A1 (en) * 2014-01-10 2016-11-17 Nanyang Technological University Embolic device, an apparatus for embolizing a target vascular site and a method thereof
CN107002168A (en) * 2014-10-22 2017-08-01 伊那维克澳大利亚有限公司 A kind of leaching simultaneously in hygrometric state solid and the METAL EXTRACTION method of absorption

Families Citing this family (59)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SE514592C2 (en) * 1998-05-18 2001-03-19 Flaekt Ab Method and apparatus for flue gas purification with extinguishing lime in immediate connection with flue gas purification
AP1421A (en) * 1999-09-07 2005-06-03 Billiton Intellectual Property B V Bioleaching of sulphide minerals.
WO2001018270A1 (en) * 1999-09-09 2001-03-15 Billiton Intellectual Property B.V. Recovery of nickel and copper from sulphide concentrates by bioleaching
AUPQ578200A0 (en) * 2000-02-22 2000-03-16 Anaconda Nickel Limited Method for the recovery of nickel and/or cobalt
US6391089B1 (en) * 2000-11-29 2002-05-21 Walter Curlook Acid leaching of nickel laterite ores for the extraction of their nickel and cobalt values
AUPR207200A0 (en) * 2000-12-13 2001-01-11 QNI Limited Hydroxide solids enrichment by slurry contact
JP4907781B2 (en) * 2001-05-14 2012-04-04 三菱化学株式会社 Method for producing compound
US6755891B2 (en) * 2002-04-16 2004-06-29 Cominco Engineering Services Ltd. Process for the treatment or removal of impurities in a hydrometallurgical extraction process
KR20020041373A (en) * 2002-05-01 2002-06-01 서영석 Metal component recovery method of semiconductor etching waste liquid
CA2387633C (en) * 2002-05-24 2011-04-26 Cominco Engineering Services Ltd. Chloride assisted hydrometallurgical extraction of metals
US20040200730A1 (en) * 2003-04-14 2004-10-14 Kyo Jibiki Hydrometallurgical copper recovery process
JP4085908B2 (en) 2003-07-28 2008-05-14 住友金属鉱山株式会社 Method for concentrating noble metals contained in leaching residue of wet copper refining process
US7799294B2 (en) * 2003-07-30 2010-09-21 Cognis Ip Management Gmbh Methods for improving the recovery of metal leaching agents
JP2005307247A (en) * 2004-04-20 2005-11-04 Sumitomo Metal Mining Co Ltd Solvent extraction method for copper
JP5151072B2 (en) * 2006-05-31 2013-02-27 トヨタ自動車株式会社 Method for recovering metal constituting electrode from lithium battery
US8252254B2 (en) 2006-06-15 2012-08-28 Barrick Gold Corporation Process for reduced alkali consumption in the recovery of silver
GB0618025D0 (en) * 2006-09-13 2006-10-25 Enpar Technologies Inc Electrochemically catalyzed extraction of metals from sulphide minerals
FR2907352B1 (en) * 2006-10-20 2009-02-20 Terra Nova PROCESS FOR PROCESSING WASTE CONTAINING PRECIOUS METALS AND DEVICE FOR CARRYING OUT SAID METHOD
CN101328536B (en) * 2007-06-18 2010-06-02 中国恩菲工程技术有限公司 Process for comprehensive recovery of nickel, copper, cobalt, sulfur and magnesium from ore
US8262768B2 (en) 2007-09-17 2012-09-11 Barrick Gold Corporation Method to improve recovery of gold from double refractory gold ores
US8003064B2 (en) 2007-09-17 2011-08-23 Freeport-Mcmoran Corporation Controlled copper leach recovery circuit
US7988938B2 (en) * 2007-12-24 2011-08-02 Bhp Billiton Ssm Development Pty Ltd. Selectively leaching cobalt from lateritic ores
CN101215638B (en) * 2008-01-11 2010-10-13 昆明理工大学 Method for eluting nickel from nickel-carrying activated carbon by washing powder solution
FI120943B (en) * 2008-02-19 2010-05-14 Norilsk Nickel Finland Oy Method for the separation of zinc, iron, calcium, copper and manganese from aqueous cobalt and / or nickel solutions
WO2009149521A1 (en) * 2008-06-13 2009-12-17 Poseidon Nickel Limited Method for the recovery of base metals from ores
JP4565025B2 (en) * 2008-07-23 2010-10-20 日鉱金属株式会社 Leaching method of copper sulfide ore using iodine
CN102099497A (en) * 2008-07-29 2011-06-15 Bhp比利通Ssm开发有限公司 Process for controlled homogeneous acid leaching
FI121180B (en) * 2008-11-03 2010-08-13 Outotec Oyj A method for treating nickel plater ore
US8052774B2 (en) 2009-03-31 2011-11-08 Sumitomo Metal Mining Co., Ltd. Method for concentration of gold in copper sulfide minerals
CN101565837B (en) * 2009-06-03 2011-01-19 北京矿冶研究总院 Method for producing electrolytic nickel by laterite nickel-cobalt enrichment
JP4950257B2 (en) * 2009-08-24 2012-06-13 Jx日鉱日石金属株式会社 Method for leaching copper laminates from copper sulfide ores
CN101792864B (en) * 2009-11-17 2012-06-27 灵宝金源矿业股份有限公司 Hyperbaric oxygen acid leaching process for cogenerating calcium sulfate whiskers from copper-sulphide ores
US8979976B2 (en) 2010-05-20 2015-03-17 Cesl Limited Solvent extraction process for separating cobalt from nickel in aqueous solution
CN102864305A (en) * 2011-07-08 2013-01-09 浙江盈联科技有限公司 Separation and purification technology of cobalt-copper alloy lixivium
US8420048B1 (en) 2011-12-20 2013-04-16 Freeport-Mcmoran Corporation System and method for parallel solution extraction of one or more metal values from metal-bearing materials
US9169533B2 (en) 2011-12-20 2015-10-27 Freeport Minerals Corporation System and method including multi-circuit solution extraction for recovery of metal values from metal-bearing materials
CN102634677B (en) * 2012-04-13 2014-01-15 金川集团有限公司 Method for recovering cobalt in cobalt-rich matte leaching liquid
US8905242B2 (en) 2012-05-25 2014-12-09 John VanDeMierden Ash processing and metals recovery systems and methods
RU2502811C1 (en) * 2012-12-19 2013-12-27 Федеральное Государственное Бюджетное Учреждение Науки Институт Химии И Химической Технологии Сибирского Отделения Российской Академии Наук (Иххт Со Ран) Method for processing of oxidised nickel ores
JP5622061B2 (en) * 2013-03-26 2014-11-12 住友金属鉱山株式会社 Method for producing hematite for iron making
FI125388B (en) * 2013-06-07 2015-09-30 Outotec Finland Oy Process for the recovery of copper and precious metals
FI20136129L (en) * 2013-11-15 2015-05-16 Outotec Finland Oy Process for the recovery of cobalt and copper
KR101399953B1 (en) * 2013-11-20 2014-05-30 한국지질자원연구원 Method for producing copper concentrates from complex copper ore
JP5800255B2 (en) * 2014-02-27 2015-10-28 住友金属鉱山株式会社 Method for producing hematite for iron making
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CN107400788B (en) * 2017-07-18 2020-05-22 中国恩菲工程技术有限公司 Method for precipitating nickel and cobalt in laterite-nickel ore hydrometallurgy
EP3794164A4 (en) 2018-05-18 2022-03-09 California Institute of Technology Process to convert reduced sulfur species and water into hydrogen and sulfuric acid
KR102178219B1 (en) * 2019-02-13 2020-11-12 고려아연 주식회사 Economical Smelting Method for Nickel from Nickel Sulfide ore, combined Hydrometallurgical and Pyrometallurgical Process
JP2022544772A (en) 2019-08-13 2022-10-21 カリフォルニア インスティチュート オブ テクノロジー Process for making calcium oxide or ordinary Portland cement from calcium-bearing rocks and minerals
CN111334664B (en) * 2020-03-07 2021-03-09 江苏北矿金属循环利用科技有限公司 Method for comprehensively recycling valuable metals from ternary lithium battery positive electrode material based on magnesium salt circulation
CN111638244B (en) * 2020-06-05 2021-05-11 中南大学 Safety analysis method for zinc concentrate oxygen pressure acid leaching high-sulfur slag
CN112575208B (en) * 2020-12-02 2021-08-24 桂林理工大学 Method for preparing high-purity manganese sulfate from electrolytic manganese sulfide slag
US11584975B1 (en) 2021-08-26 2023-02-21 Sherritt International Corporation Integrated pressure oxidative leach of copper sulphidic feed with copper heap leach
JP2024534532A (en) * 2021-09-20 2024-09-20 ゲリオン・テクノロジーズ・ピーティーワイ・リミテッド Recycling method for recovering valuable metal elements from iron-contaminated process streams

Family Cites Families (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3466144A (en) * 1967-07-03 1969-09-09 American Metal Climax Inc Treatment of nickeliferous oxidic materials for the recovery of nickel values
CA938794A (en) * 1968-12-13 1973-12-25 Weston David Hydrometallurgical treatment of nickel group ores
US3870585A (en) * 1973-02-15 1975-03-11 Pureco Systems Inc Apparatus and method for evaporative concentration of aqueous solutions and slurries
US4039406A (en) 1973-08-10 1977-08-02 Noranda Mines Limited Recovering copper from concentrates with insoluble sulfate forming leach
US4044096A (en) * 1975-12-11 1977-08-23 Amax Inc. Sulfuric acid leaching of nickeliferous laterite
JPS5942737B2 (en) * 1979-12-26 1984-10-17 三菱マテリアル株式会社 Method for recovering valuable metals from acid leaching solution of manganese nodule
ZW3481A1 (en) * 1980-02-18 1981-05-20 Nat Inst Metallurg The leaching of sulphidic mattes containing non-ferrous metals and iron
CA1150062A (en) 1980-06-10 1983-07-19 Robert W. Stanley Hydrometallurgical treatment of copper-bearing hematite residue
CA1171287A (en) * 1980-11-05 1984-07-24 William R. Hatch Acid leaching of lateritic nickel ores
US4435369A (en) * 1981-06-22 1984-03-06 Simpson Charles H Hydrometallurgical process for extraction of nickel
JPS5947338A (en) * 1982-09-10 1984-03-17 Sumitomo Metal Mining Co Ltd Method for removing iron from acidic solution containing nickel and cobalt
CA1206339A (en) * 1983-03-29 1986-06-24 Donald R. Weir Recovery of cobalt and nickel from sulphidic material
JPH04236792A (en) * 1991-01-21 1992-08-25 Hitachi Cable Ltd Production of high purity electrolytic copper
US5431788A (en) * 1993-06-28 1995-07-11 Cominco Engineering Services Ltd. Chloride assisted hydrometallurgical copper extraction
US5650057A (en) * 1993-07-29 1997-07-22 Cominco Engineering Services Ltd. Chloride assisted hydrometallurgical extraction of metal
US5855858A (en) * 1993-07-29 1999-01-05 Cominco Engineering Services Ltd. Process for the recovery of nickel and/or cobalt from an ore or concentrate
CA2137124C (en) * 1994-12-01 1999-03-16 Tao Xue Pressure leaching of nickel and cobalt sulphides with chlorine under controlled redox potential conditions

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090241736A1 (en) * 2008-03-27 2009-10-01 Nippon Mining & Metals Co., Ltd. Method for recovering metal from ore
US8585798B2 (en) 2008-03-27 2013-11-19 Nippon Mining & Metals Co., Ltd. Method for recovering metal from ore
AU2008264193B1 (en) * 2008-08-11 2009-05-21 Jx Nippon Mining & Metals Corporation Process for recovery of copper from copper-containing chloride media
US20100031779A1 (en) * 2008-08-11 2010-02-11 Nippon Mining & Metals Co., Ltd. Process for recovery of copper from copper-containing chloride media
US9234259B2 (en) 2008-08-11 2016-01-12 Jx Nippon Mining & Metals Corporation Process for recovery of copper from copper-containing chloride media
WO2013163712A1 (en) 2012-05-04 2013-11-07 Vale S.A. Sulfide ore leaching process
WO2014023755A1 (en) * 2012-08-10 2014-02-13 Basf Se Metal leach and recovery process
AU2013301565B2 (en) * 2012-08-10 2016-02-25 Basf Se Metal leach and recovery process
EA026159B1 (en) * 2012-08-10 2017-03-31 Басф Се Metal leach and recovery process
US9657368B2 (en) 2012-08-10 2017-05-23 Basf Se Metal leach and recovery process
US20160331380A1 (en) * 2014-01-10 2016-11-17 Nanyang Technological University Embolic device, an apparatus for embolizing a target vascular site and a method thereof
CN107002168A (en) * 2014-10-22 2017-08-01 伊那维克澳大利亚有限公司 A kind of leaching simultaneously in hygrometric state solid and the METAL EXTRACTION method of absorption

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